CN103387248A - Method and fluidized-bed plant for preparing magnesium sulfate monohydrate by using magnesium sulfate heptahydrate - Google Patents
Method and fluidized-bed plant for preparing magnesium sulfate monohydrate by using magnesium sulfate heptahydrate Download PDFInfo
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- CN103387248A CN103387248A CN2013103203681A CN201310320368A CN103387248A CN 103387248 A CN103387248 A CN 103387248A CN 2013103203681 A CN2013103203681 A CN 2013103203681A CN 201310320368 A CN201310320368 A CN 201310320368A CN 103387248 A CN103387248 A CN 103387248A
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Abstract
The invention discloses a method for preparing magnesium sulfate monohydrate by using magnesium sulfate heptahydrate. The method is characterized in that magnesium sulfate heptahydrate material sequentially pass through at least two fluidized beds of which the bed body temperatures are increased gradually so that the magnesium sulfate heptahydrate material is dehydrated step by step, thus obtaining the magnesium sulfate heptahydrate, wherein the bed body temperatures of the fluidized beds are controlled in a range of 50-200 DEG C. According to the method, the multi-chamber fluidized beds are utilized to dry the magnesium sulfate monohydrate and the magnesium sulfate monohydrate is dehydrated step by step to prepare the magnesium sulfate heptahydrate, so that the drying temperature is easily controlled, the dehydration effect is good, the process flow is simple, energy-saving and environment-friendly, and the economic benefit is excellent.
Description
Technical field
The present invention relates to the production technique of sal epsom, be specifically related to prepare from magnesium sulfate heptahydrate the method for magnesium sulfate monohydrate, and many furnace chambers fluidized bed plant.
Background technology
Sal epsom is a kind of pair of nutrient fertilizer,, because sulphur, magnesium are moderate-element in crop, is widely used in the middle of agriculture production at present.Common sal epsom is mainly magnesium sulfate heptahydrate and magnesium sulfate monohydrate two series products, wherein its water ratio of magnesium sulfate monohydrate is low, sulphur, Mg content are high, and can be used for fertilizer additive to prevent the piece that hardens into of fertilizer, demand for magnesium sulfate monohydrate increases gradually both at home and abroad, has boundless market outlook and powerful application potential.
Present stage, the production technique of magnesium sulfate monohydrate mainly contains sulfuric acid process, evaporation and hot melt and soaks the method three major types.Wherein sulfuric acid process is to make the vitriol oil and light burnt powder (magnesia) or the magnesite direct reaction through pulverizing, and obtains magnesium sulfate monohydrate, then through super-dry, obtains product; Evaporation mainly heats the magnesium sulfate heptahydrate solid by intensification, controls the heating condition to magnesium sulfate heptahydrate, make its gradually drying obtain the sulfuric acid monohydrate magnesium products; It is the bittern of evaporating brine for salt lake or seawater that hot melt soaks rule, with the high temp. salt (MgSO that separates out in its evaporative process
4Content 〉=30%) with the magnesium chloride solution leaching, then, through the insulation clarification, then by crystallizing and drying, obtain the sulfuric acid monohydrate magnesium products.
Evaporation is relatively simple because of its technique, and products obtained therefrom purity is high and energy input is lower, and the most common.Magnesium sulfate heptahydrate is in heat-processed, and different temperature condition has very significantly difference for its dehydration characteristic: dissolve in self crystal water 67.5 ℃ of left and right, easily decompose; In the time of 70-80 ℃, lose 4 crystal water; Lose 5 crystal water in the time of 100 ℃; Lose 6 crystal water in the time of 150 ℃; Lose whole crystal water in the time of 200 ℃.Thereby, prepare magnesium sulfate monohydrate by the method that dehydrates, it is extremely important that the selection of drying process seems.
Existing drying process mainly is divided into rotary drying method, rotary flashing drying method, fluid-bed drying etc.Wherein, the rotary drying method, because the residence time of material is long, causes drying temperature wayward, to the also just more difficult control of dehydration of magnesium sulfate heptahydrate, so this method is not suitable for the production of magnesium sulfate monohydrate; Rotary flashing drying method (CN201210040066.4) need to be processed magnesium sulfate heptahydrate in Rotatingandflashstreamingdrier, complex technical process, energy consumption are larger, and the cost that the method prepares magnesium sulfate monohydrate is higher, economical effectiveness is not good; Traditional fluid-bed drying,, if the granularity of magnesium sulfate heptahydrate is less, water content is higher, " press " phenomenon that the material caking causes easily occurs, and affects the dewatering efficiency in fluid mapper process.
Therefore, also need a kind of improved method to be used for preparing magnesium sulfate monohydrate from magnesium sulfate heptahydrate.
Summary of the invention
The present invention is intended to solve existing evaporation and prepares magnesium sulfate monohydrate complex process, high in cost of production shortcoming, and a kind of improved method is provided, and is used for preparing magnesium sulfate monohydrate from magnesium sulfate heptahydrate.
Technical scheme of the present invention comprises a kind of for prepare the method for magnesium sulfate monohydrate from magnesium sulfate heptahydrate, comprise: at least two fluidized-beds that the magnesium sulfate heptahydrate material is raise gradually through the bed temperature successively, to dewater step by step, obtain magnesium sulfate monohydrate, the bed temperature of wherein said fluidized-bed is the scope of 50-200 ℃.
In some embodiment, before described method also is included in charging, with the broken of magnesium sulfate heptahydrate and screening step.
Preferably, through the particle diameter of the described magnesium sulfate heptahydrate material of broken and screening less than or equal to 5mm.
In some embodiment, described method comprises makes the magnesium sulfate heptahydrate material successively through a fluidized-bed, No. two fluidized-beds and No. three fluidized-beds, and the bed temperature of a described fluidized-bed, No. two fluidized-beds and No. three fluidized-beds is respectively 50-100 ℃, 50-100 ℃ and 160-220 ℃.
In some embodiment, described method can also comprise the recycling step that uses fly-ash separator to reclaim tiny material.
Described magnesium sulfate heptahydrate material can be 2-4 minute in the residence time of a fluidized-bed; Described material can be 4-6 minute in the residence time of No. two fluidized-beds; Described material can be 2-3 minute in the residence time of No. three fluidized-beds.
In some embodiment, the blast velocity of a described fluidized-bed, No. two fluidized-beds and No. three fluidized-beds can be 15-30m
3/ s; The air inducing speed of a described fluidized-bed, No. two fluidized-beds and No. three fluidized-beds can be 20-35m
3/ s.
In some embodiment, the input speed of described sal epsom material can be 10-30m/ minute.
The present invention also provides a kind of many furnace chambers fluidized bed plant, comprises the fluidized-bed of at least two series connection, and the bed temperature of described fluidized-bed raises successively, and the bed temperature of each described fluidized-bed is independent adjustable.
Preferably, described many furnace chambers fluidized bed plant comprises a fluidized-bed of series connection, No. two fluidized-beds and No. three fluidized-beds, and the bed temperature of a described fluidized-bed, No. two fluidized-beds, No. three fluidized-beds is adjustable in the scope of 50-100 ℃, 50-100 ℃ and 160-220 ℃ respectively.
The present invention utilizes many furnace chambers fluidised bed drying magnesium sulfate heptahydrate,, through the substep dehydration, prepares magnesium sulfate monohydrate, is easy to control drying temperature, and dehydrating effect is good, and technical process is simple, energy-conserving and environment-protective, and economic benefit is excellent.
Description of drawings
Fig. 1 illustrates according to one exemplary embodiment of the present invention, is used for preparing from magnesium sulfate heptahydrate the process flow sheet of magnesium sulfate monohydrate.
Embodiment
The present invention utilizes many furnace chambers fluidised bed drying magnesium sulfate heptahydrate, prepares the technique of magnesium sulfate monohydrate through the substep dehydration.The fluidized bed plant that uses has unique structure design, and it comprises the fluidized-bed of at least two series connection, and the bed temperature of fluidized-bed raises successively, and each fluidized-bed all has independent adjustable bed temperature.This design can realize the dry step by step of magnesium sulfate heptahydrate, helps to improve common " press " phenomenon of fluid-bed drying.
The fluid bed furnace cavity temperature of connecting by adjusting, and control air inducing speed, blast velocity and the input speed of whole fluidized bed plant, and the residence time of each section fluidisation, control the degree of drying to the magnesium sulfate heptahydrate wet feed, can control well the purity of sulfuric acid monohydrate magnesium products.
As the preferred embodiments of the present invention, be used for can comprising from many furnace chambers fluidized bed plant that magnesium sulfate heptahydrate prepares magnesium sulfate monohydrate the fluidized-bed of three series connection: a fluidized-bed, No. two fluidized-beds and No. three fluidized-beds, its temperature are adjustable in the scope of 50-100 ℃, 50-100 ℃ and 160-220 ℃ respectively.
Fig. 1 is according to a preferred embodiment of the invention schematically illustrated, is used for preparing from magnesium sulfate heptahydrate the process flow sheet of magnesium sulfate monohydrate.
As seen from the figure, used the fluidized-bed of three series connection in this embodiment, the magnesium sulfate heptahydrate wet feed is carried out three sections processed step by step.The magnesium sulfate heptahydrate wet feed carries out fluidisation successively in a fluidized-bed, No. two fluidized-beds, No. three fluidized-beds, and collects the sulfuric acid monohydrate magnesium products in holding tank.
The bed temperature of three fluidized-beds raises successively, and its temperature range is separately positioned on 50-100 ℃, 100-160 ℃ and 160-220 ℃.The blast velocity of fluidized bed plant can be controlled at 15-30m
3/ s, air inducing speed can be controlled at 20-35m
3/ s.
Before charging, can carry out preheating to fluidized-bed, so that its temperature reaches preset value.For example, be respectively 15-30m by controlling air blast and air inducing speed
3/ s and 20-35m
3/ s, set the intake air temperature of each fluidized-bed furnace chamber, simultaneously with air heating.
The bed temperature for the treatment of each fluidized-bed reaches preset value
The magnesium sulfate heptahydrate wet feed, from a fluidized-bed charging, for example can be transported to the magnesium sulfate heptahydrate wet feed in fluidized-bed by feeding screw, and its input speed is controlled can be 10-30m/ minute.
Owing to easily luming during the magnesium sulfate heptahydrate raw material storage, for fear of excessive " press " phenomenon that causes of wet stock particle diameter, can first to magnesium sulfate heptahydrate, carry out fragmentation and screening processing, sieve out the large granular materials of particle diameter excessive (for example greater than 5mm), improve the fluidization efficiency of fluidized-bed.For example, can use small-sized crusher in crushing magnesium sulfate heptahydrate, use subsequently large-scale mesh screen (for example 25 orders) to sieve through broken magnesium sulfate heptahydrate material, keep fines to treat fluidized drying.
In the segmentation fluid mapper process, control the residence time of material in each fluidized-bed, for example can control it at first be 2-4 minute in the residence time of a fluidized-bed; Enter afterwards fluidized-bed No. two, the residence time is 4-6 minute; Come finally fluidized-bed No. three, the residence time is 2-3 minute.
In the discharging stage, the material after fluidised bed drying (sulfuric acid monohydrate magnesium products) sinks in holding tank finally, collects to a certain degree afterwards from discharge hole for discharge and cooling packing.
Can utilize fly-ash separator (for example, tornado dust collector) to reclaim the powder material that air blast is taken out of, and collect in sack cleaner, to reduce loss and the dust pollution of powder material.
The sulfuric acid monohydrate magnesium products pattern that the method according to this invention prepares is oblique shape or the crystallization of batter post shape, particulate state white powder, and its water content is in 13-15(weight) adjustable in the scope of %, median size is usually adjustable in the scope of 100-500 μ m.
To sum up, the invention provides a kind of for prepare the method for magnesium sulfate monohydrate from magnesium sulfate heptahydrate, and corresponding many furnace chambers fluidized bed plant.Wherein, the magnesium sulfate heptahydrate material enters the fluidized-bed of at least two (being preferably three) series connection successively, because the furnace chamber temperature of each fluidized-bed can independently be controlled, by regulating the temperature of each section fluid mapper process, can realize the dehydration step by step to magnesium sulfate heptahydrate, make the drying effect of magnesium sulfate heptahydrate easily control.
This operation of magnesium sulfate heptahydrate being carried out the substep dehydration, can avoid wet stock to lump due to fast dewatering and cause " press phenomenon ", can't be for the present situation of magnesium sulfate heptahydrate wet stock drying with thoroughly solving fluidization.
Fluid-bed drying is easy to control, technique is relatively simple, energy-conserving and environment-protective.Compare with technology of preparing, the magnesium sulfate heptahydrate convection drying evaporation of other existing magnesium sulfate monohydrates, preparation method's cost of the present invention is lower, economic benefit is excellent.
Below in conjunction with specific embodiment, the present invention is described in further detail.
Embodiment 1:
Magnesium sulfate heptahydrate wet feed: in small-sized crusher, the magnesium sulfate heptahydrate of part caking is carried out fragmentation, will sieve through broken magnesium sulfate heptahydrate material with the 25 large-scale mesh screens of purpose subsequently, keep fines to treat fluidized drying.
Fluidized-bed preheating: control air blast and air inducing speed and be respectively 15m
3/ s and 20m
3/ s, the bed temperature of setting one to No. three fluidized-bed is respectively 50 ℃, 100 ℃ and 160 ℃, opens the blast heating switch with air heating.
Charging: after each fluidized bed temperature reaches desired value, start to feed in raw material.Screening magnesium sulfate heptahydrate wet feed is later sent in charging opening, and material is transported in fluidized-bed by feeding screw, and its input speed is controlled to be 30m/ minute.
The segmentation fluidisation: the magnesium sulfate heptahydrate wet feed is successively a fluidized-bed fluidisation, 4 minutes residence time; Enter afterwards fluidized-bed No. two, 6 minutes residence time; Enter finally fluidized-bed No. three, the residence time is 3 minutes.
Discharging and vent gas treatment discharge process: the material after fluidised bed drying sinks in the middle of holding tank, collects to a certain degree afterwards from discharge hole for discharge and cooling packing; Tornado dust collector reclaim the powder material that air blast is taken out of, then with sack cleaner, reclaim tiny dust.
The water content of this embodiment gained sulfuric acid monohydrate magnesium products is 14.50%, and the product pattern is oblique shape or the crystallization of batter post shape, particulate state white powder, and Average Particle Diameters is 400-500 μ m.
Embodiment 2:
Magnesium sulfate heptahydrate wet feed: in small-sized crusher, the magnesium sulfate heptahydrate of part caking is carried out fragmentation, will sieve through broken magnesium sulfate heptahydrate material with the 25 large-scale mesh screens of purpose subsequently, keep fines to treat fluidized drying.
Fluidized-bed preheating: control air blast and air inducing speed and be respectively 20m
3/ s and 30m
3/ s, set one to No. three furnace chamber temperature and be respectively 70 ℃, 120 ℃ and 180 ℃, and open the blast heating switch with air heating.
Charging: after each fluidized bed temperature reaches desired value, start to feed in raw material, screening magnesium sulfate heptahydrate wet feed is later sent in charging opening, material is transported in fluidized-bed by feeding screw, and its input speed is controlled to be 20m/ minute.
The segmentation fluidisation: the magnesium sulfate heptahydrate wet feed is successively a fluidized-bed fluidisation, 3 minutes residence time; Enter afterwards fluidized-bed No. two, 5 minutes residence time; Enter finally fluidized-bed No. three, the residence time is 3 minutes.
Discharging and vent gas treatment discharge process: the material after fluidised bed drying sinks in the middle of holding tank, collects to a certain degree afterwards from discharge hole for discharge and cooling packing; Tornado dust collector reclaim the powder material that air blast is taken out of, then with sack cleaner, reclaim tiny dust.
The water content of this embodiment gained sulfuric acid monohydrate magnesium products is 13.82%, and the product pattern is oblique shape or the crystallization of batter post shape, particulate state white powder, and Average Particle Diameters is 300-400 μ m.
Embodiment 3:
Magnesium sulfate heptahydrate wet feed: in small-sized crusher, the magnesium sulfate heptahydrate of part caking is carried out fragmentation, will sieve through broken magnesium sulfate heptahydrate material with the 25 large-scale mesh screens of purpose subsequently, keep fines to treat fluidized drying.
Fluidized-bed preheating: control air blast and air inducing speed and be respectively 25m
3/ s and 25m
3/ s, set one to No. three furnace chamber temperature and be respectively 90 ℃, 140 ℃ and 200 ℃, and open the blast heating switch with air heating.
Charging: after each fluidized bed temperature reaches desired value, start to feed in raw material, screening magnesium sulfate heptahydrate wet feed is later sent in charging opening, material is transported in fluidized-bed by feeding screw, and its input speed is controlled to be 20m/ minute.
The segmentation fluidisation: the magnesium sulfate heptahydrate wet feed is successively a fluidized-bed fluidisation, 3 minutes residence time; Enter afterwards fluidized-bed No. two, 5 minutes residence time; Enter finally fluidized-bed No. three, the residence time is 2 minutes.
Discharging and vent gas treatment discharge process: the material after fluidised bed drying sinks in the middle of holding tank, collects to a certain degree afterwards from discharge hole for discharge and cooling packing; Tornado dust collector reclaim the powder material that air blast is taken out of, then with sack cleaner, reclaim tiny dust.
The water content of this embodiment gained sulfuric acid monohydrate magnesium products is 13.05%, and the product pattern is oblique shape or the crystallization of batter post shape, particulate state white powder, and Average Particle Diameters is 200-300 μ m.
Embodiment 4:
Magnesium sulfate heptahydrate wet feed: in small-sized crusher, the magnesium sulfate heptahydrate of part caking is carried out fragmentation, will sieve through broken magnesium sulfate heptahydrate material with the 25 large-scale mesh screens of purpose subsequently, keep fines to treat fluidized drying.
Fluidized-bed preheating: control air blast and air inducing speed and be respectively 30m
3/ s and 35m
3/ s, set one to No. three furnace chamber temperature and be respectively 100 ℃, 160 ℃ and 220 ℃, and open the blast heating switch with air heating.
Charging: after each fluidized bed temperature reaches desired value, start to feed in raw material, screening magnesium sulfate heptahydrate wet feed is later sent in charging opening, material is transported in fluidized-bed by feeding screw, and its input speed is controlled to be 10m/ minute.
The segmentation fluidisation: the magnesium sulfate heptahydrate wet feed is successively a fluidized-bed fluidisation, 2 minutes residence time; Enter afterwards fluidized-bed No. two, 4 minutes residence time; Enter finally fluidized-bed No. three, the residence time is 2 minutes.
Discharging and vent gas treatment discharge process: the material after fluidised bed drying sinks in the middle of holding tank, collects to a certain degree afterwards from discharge hole for discharge and cooling packing; Tornado dust collector reclaim the powder material that air blast is taken out of, then with sack cleaner, reclaim tiny dust.
The water content of this embodiment gained sulfuric acid monohydrate magnesium products is 14.15%, and the product pattern is oblique shape or the crystallization of batter post shape, particulate state white powder, and Average Particle Diameters is 100-200 μ m.
The above the specific embodiment of the present invention, do not form the restriction to protection domain of the present invention.Various other corresponding changes and distortion that any technical conceive according to the present invention has been done, all should be included in the protection domain of the claims in the present invention.
Claims (13)
1. method that is used for preparing from magnesium sulfate heptahydrate magnesium sulfate monohydrate, it is characterized in that, described method comprises: at least two fluidized-beds that the magnesium sulfate heptahydrate material is raise gradually through the bed temperature successively, to dewater step by step, obtain magnesium sulfate monohydrate, the bed temperature of wherein said fluidized-bed is the scope of 50-200 ℃.
2. the method for claim 1, comprise and make the magnesium sulfate heptahydrate material successively through a fluidized-bed, No. two fluidized-beds and No. three fluidized-beds, and the bed temperature of a described fluidized-bed, No. two fluidized-beds and No. three fluidized-beds is respectively 50-100 ℃, 50-100 ℃ and 160-220 ℃.
3. the method for claim 1, wherein described method also comprises the step magnesium sulfate heptahydrate material is broken and that sieve.
4. method as claimed in claim 3, wherein, through the particle diameter of the described magnesium sulfate heptahydrate material of broken and screening less than or equal to 5mm.
5. the method for claim 1, wherein described method also comprises the recycling step that uses fly-ash separator to reclaim tiny material.
6. the method for claim 1, wherein described magnesium sulfate heptahydrate material is 2-4 minute in the residence time of a fluidized-bed.
7. the method for claim 1, wherein described material is 4-6 minute in the residence time of No. two fluidized-beds.
8. the method for claim 1, wherein described material is 2-3 minute in the residence time of No. three fluidized-beds.
9. the method for claim 1, wherein the blast velocity of a described fluidized-bed, No. two fluidized-beds and No. three fluidized-beds is 15-30m
3/ s.
10. the method for claim 1, wherein the air inducing speed of a described fluidized-bed, No. two fluidized-beds and No. three fluidized-beds is 20-35m
3/ s.
11. the method for claim 1, wherein the input speed of described sal epsom material is 10-30m/ minute.
12. more than one kind, the furnace chamber fluidized bed plant, is characterized in that, comprises the fluidized-bed of at least two series connection, the bed temperature of described fluidized-bed raises successively, and the bed temperature of each described fluidized-bed is independent adjustable.
13. many furnace chambers fluidized bed plant as claimed in claim 12, comprise a fluidized-bed of series connection, No. two fluidized-beds and No. three fluidized-beds, and the bed temperature of a described fluidized-bed, No. two fluidized-beds, No. three fluidized-beds is adjustable in the scope of 50-100 ℃, 50-100 ℃ and 160-220 ℃ respectively.
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103708509A (en) * | 2013-12-20 | 2014-04-09 | 杨海基 | Method for producing magnesium sulfate monohydrate by using spray drying process |
| CN105651003A (en) * | 2016-01-22 | 2016-06-08 | 青岛华仁太医药业有限公司 | Boiling and drying technology for Puyuan Hewei capsule particles |
| CN109534374A (en) * | 2018-12-05 | 2019-03-29 | 许昌豫通生物科技有限公司 | A kind of production technology of anhydrous magnesium sulfate |
| CN110803878A (en) * | 2019-11-25 | 2020-02-18 | 江苏一夫科技股份有限公司 | Device and method for producing II type anhydrous gypsum by using phosphogypsum |
| CN115031519A (en) * | 2022-07-11 | 2022-09-09 | 吴江市威士达铜业科技有限公司 | Production method and production device of copper sulfate monohydrate |
| CN115353131A (en) * | 2022-09-14 | 2022-11-18 | 丹东金辽化工有限公司 | Production method of magnesium sulfate monohydrate |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5281242A (en) * | 1991-06-10 | 1994-01-25 | Exportadora De Sal, S.A De C.V. | Method for recovering magnesium sulfate products from mixtures of epsomite and halite |
| CN1544331A (en) * | 2003-11-14 | 2004-11-10 | 天津市昌昊化工股份合作公司 | Magnesium sulfate production method using magnesium oxide and desulfurated waste fluid |
| CN102583459A (en) * | 2012-02-22 | 2012-07-18 | 化工部长沙设计研究院 | Process for preparing magnesium sulfate monohydrate by using water-containing magnesium sulfate heptahydrate |
| CN202501712U (en) * | 2012-02-10 | 2012-10-24 | 沈阳一通创业干燥设备有限公司 | Vibrated fluidized bed dryer |
-
2013
- 2013-07-29 CN CN201310320368.1A patent/CN103387248B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5281242A (en) * | 1991-06-10 | 1994-01-25 | Exportadora De Sal, S.A De C.V. | Method for recovering magnesium sulfate products from mixtures of epsomite and halite |
| CN1544331A (en) * | 2003-11-14 | 2004-11-10 | 天津市昌昊化工股份合作公司 | Magnesium sulfate production method using magnesium oxide and desulfurated waste fluid |
| CN202501712U (en) * | 2012-02-10 | 2012-10-24 | 沈阳一通创业干燥设备有限公司 | Vibrated fluidized bed dryer |
| CN102583459A (en) * | 2012-02-22 | 2012-07-18 | 化工部长沙设计研究院 | Process for preparing magnesium sulfate monohydrate by using water-containing magnesium sulfate heptahydrate |
Non-Patent Citations (2)
| Title |
|---|
| 李晓梅: "温度对生产MgSO4•H2O 流态化干燥的影响", 《中国井矿盐》, vol. 32, no. 4, 31 July 2001 (2001-07-31), pages 21 - 23 * |
| 郭安强等: "流化床干燥装置在MgSO4•H2O生产中的应用", 《无机盐工业》, no. 3, 31 December 1996 (1996-12-31), pages 45 - 47 * |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103708509A (en) * | 2013-12-20 | 2014-04-09 | 杨海基 | Method for producing magnesium sulfate monohydrate by using spray drying process |
| CN103708509B (en) * | 2013-12-20 | 2015-09-16 | 杨海基 | A kind of spray-drying process produces the method for magnesium sulfate monohydrate |
| CN105651003A (en) * | 2016-01-22 | 2016-06-08 | 青岛华仁太医药业有限公司 | Boiling and drying technology for Puyuan Hewei capsule particles |
| CN105651003B (en) * | 2016-01-22 | 2018-10-19 | 青岛华仁太医药业有限公司 | A kind of fluidized drying technique of Pu Yuan and capsule for treating gastropathy particle |
| CN109534374A (en) * | 2018-12-05 | 2019-03-29 | 许昌豫通生物科技有限公司 | A kind of production technology of anhydrous magnesium sulfate |
| CN110803878A (en) * | 2019-11-25 | 2020-02-18 | 江苏一夫科技股份有限公司 | Device and method for producing II type anhydrous gypsum by using phosphogypsum |
| CN115031519A (en) * | 2022-07-11 | 2022-09-09 | 吴江市威士达铜业科技有限公司 | Production method and production device of copper sulfate monohydrate |
| CN115353131A (en) * | 2022-09-14 | 2022-11-18 | 丹东金辽化工有限公司 | Production method of magnesium sulfate monohydrate |
| CN115353131B (en) * | 2022-09-14 | 2023-09-12 | 丹东金辽化工有限公司 | Production method of magnesium sulfate monohydrate |
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